WO2014170729A1 - Procédé et dispositif de fabrication de clinker - Google Patents

Procédé et dispositif de fabrication de clinker Download PDF

Info

Publication number
WO2014170729A1
WO2014170729A1 PCT/IB2014/000500 IB2014000500W WO2014170729A1 WO 2014170729 A1 WO2014170729 A1 WO 2014170729A1 IB 2014000500 W IB2014000500 W IB 2014000500W WO 2014170729 A1 WO2014170729 A1 WO 2014170729A1
Authority
WO
WIPO (PCT)
Prior art keywords
exhaust gas
furnace
flow
cyclone
gas
Prior art date
Application number
PCT/IB2014/000500
Other languages
German (de)
English (en)
Inventor
Urs Gasser
Original Assignee
Holcim Technology Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority to US14/784,331 priority Critical patent/US10106459B2/en
Priority to CN201480034076.4A priority patent/CN105283428A/zh
Priority to BR112015026061A priority patent/BR112015026061A2/pt
Priority to MA38545A priority patent/MA38545B1/fr
Priority to MX2015014419A priority patent/MX364902B/es
Priority to CA2909358A priority patent/CA2909358A1/fr
Application filed by Holcim Technology Ltd filed Critical Holcim Technology Ltd
Priority to KR1020157032680A priority patent/KR20150143777A/ko
Priority to EP14723880.2A priority patent/EP2986579B1/fr
Priority to RU2015148947A priority patent/RU2638059C2/ru
Publication of WO2014170729A1 publication Critical patent/WO2014170729A1/fr
Priority to PH12015502364A priority patent/PH12015502364A1/en
Priority to US16/139,666 priority patent/US20190039949A1/en

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
    • C04B7/44—Burning; Melting
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
    • C04B7/47—Cooling ; Waste heat management
    • C04B7/475—Cooling ; Waste heat management using the waste heat, e.g. of the cooled clinker, in an other way than by simple heat exchange in the cement production line, e.g. for generating steam
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
    • C04B7/432—Preheating without addition of fuel
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
    • C04B7/434—Preheating with addition of fuel, e.g. calcining
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
    • C04B7/44—Burning; Melting
    • C04B7/4407—Treatment or selection of the fuel therefor, e.g. use of hazardous waste as secondary fuel ; Use of particular energy sources, e.g. waste hot gases from other processes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B23/00—Heating arrangements
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/004—Systems for reclaiming waste heat
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B2290/00—Organisational aspects of production methods, equipment or plants
    • C04B2290/20—Integrated combined plants or devices, e.g. combined foundry and concrete plant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
    • F27B7/2016—Arrangements of preheating devices for the charge
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P40/00—Technologies relating to the processing of minerals
    • Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
    • Y02P40/121—Energy efficiency measures, e.g. improving or optimising the production methods

Definitions

  • the invention relates to a process for cement clinker production in which raw meal is preheated with the hot exhaust gases of a clinker furnace in a preheater and the preheated and optionally calcined in a calciner raw meal in clinker kiln is fired to clinker ' , wherein the preheater at least one strand of a Includes a plurality of sequentially flowed through by the furnace exhaust gas cyclone Schwebegas139 (2004)n in which the raw meal is preheated in stages.
  • the invention relates to a cement clinker production plant, comprising a clinker furnace, at the output side end of a clinker cooler is connected and at the task seifigem end a preheater and possibly a Kalzinator are connected, the preheater at least one strand of a plurality of successively from comprising the kiln exhaust gas along a flow path through which can flow cyclone Schwebegas139 (2004)ern in which the raw meal is preheated in stages.
  • the ABGA ⁇ se of the rotary kiln are controlled by a kiln inlet chamber and a flow constriction located above ge ⁇ leads to the calciner, to flow through them and, together with the quay in Zinator generated exhaust gas, consisting of flue gas from the calculator fuel and C02, discharged into the preheater.
  • the preheater consists of one or more strands and each strand of several heat exchanger stages, each of which is formed by a cyclone suspension gas heat exchanger.
  • the dry cement raw meal is fed to the riser pipe of the uppermost heat exchanger stage, passes through the heat exchanger stages from top to bottom and is passed from the second lowest heat exchanger stage into the calciner.
  • the hot raw meal is almost completely deacidified and flows with the calciner exhaust gas in the lowest heat exchanger stage, is deposited there, abandoned the kiln inlet chamber and passes through them as hot meal in the rotary kiln.
  • the hot meal is burned in the rotary kiln through the sintering process to clinker.
  • Kalzinatorabgas of about 1.4 normal m 3 / kg clinker from 850 to 890 ° C thermal. Energy is released step by step into the fresh raw meal in DC heat exchange. In this case, with increasing number of heat exchanger stages, the exhaust gas temperature is lower, the thermal efficiency of the furnace better and the heat exchanger tower larger and more expensive. Typically, 4 to 6 such stages are built, with the number of stages depending primarily on the raw material moisture.
  • the usable heat contained in the exhaust gas of the clinker furnace and calciner exceeds the capacity of the raw meal due to the usual quantity ratio and the characteristics of the multi-stage heat exchange. Therefore, the thermal energy of approx. 1.5 normal m 3 / kg clinker from 290 to> 350 ° C present at the kiln gas outlet of the preheater still represents a usable residual heat potential. This can be used for raw material and fuel pulp drying and otherwise, eg power generation, be used outside of the thermal process on.
  • the furnace exhaust gas is drawn through the heat exchanger stages by means of an induced draft fan. Since the entire kiln exhaust gas quantity is drawn through all heat exchanger stages, the fluidic cross sections of the heat exchanger stages are to be dimensioned as large as possible in order to minimize the pressure drop and thus the electrical energy requirement of the induced draft blower. However, this is offset by the directly dependent on the size of investment costs.
  • the present invention therefore aims to develop a method and a cement clinker production plant of the type mentioned in that the equipment costs can be reduced without having to compromise on the thermal efficiency of the furnace plant to accept.
  • the invention provides in a method of the type mentioned above, that a partial flow of the kiln exhaust gas is diverted so that only. a remaining residual stream of the kiln exhaust gas is used to preheat the 'raw meal.
  • a partial flow of the kiln exhaust gas is diverted so that only. a remaining residual stream of the kiln exhaust gas is used to preheat the 'raw meal.
  • Compared to conventional systems can thus be the same amount of raw meal with less kiln exhaust gas or preheated with the same amount of kiln exhaust gas, a larger amount of raw meal.
  • This causes relatively more heat to be withdrawn from the residual exhaust gas remaining stream used for the preheating and the kiln exhaust gas temperature to be correspondingly lower after the last heat exchanger stage, ie when leaving the preheater.
  • the temperature gradient across each heat exchanger stage is greater.
  • the non-preheating branched partial stream of kiln exhaust gas is available for thermal utilization at a temperature of 850 to 890 ° C, especially if, as is the case with a preferred procedure, the partial exhaust stream of the kiln exhaust gas follows. Seen in the flow direction of the furnace exhaust gas first, ie lowest, cyclone Schwebegastage (2004) is diverted. In particular, the partial flow of the kiln exhaust gas is branched off here between the first and second cyclone suspended gas heat exchangers, viewed in the flow direction of the kiln exhaust gas.
  • the size of the diverted partial flow can be selected according to the respective ratios, with certain limits being set up to ensure the maintenance of the overall thermal efficiency. Preference is therefore provided,.
  • the volume ratio of diverted partial flow and remaining residual flow of the .Ofenabgases is 1:99 to 40:60, preferably 10:90 to 30:70.
  • the invention is particularly advantageous for increasing the capacity of existing furnaces, with a strong increase in the use of alternative fuels and possibly even for new installations.
  • Another advantage is the separate discharge of usable heat at a much higher and thus more valuable temperature level of about 850 ° C instead of the 300 to 350 ° C usually available from the heat exchanger exhaust.
  • the diversion of a high-temperature partial gas stream can avoid costly enlargement of the existing preheater, which also results in the interruption of several weeks' operation. reduced to a few days. Then only the gas branching and the associated installations such as mixing cyclones, hot gas flaps and blowers have to be retrofitted.
  • the invention makes it possible to get to grips with the problem of the so-called AFR surcharge in the heat exchanger dimensioning and the associated additional investment.
  • the AFR surcharge is related to the use of Alternative Fuels and Raw Materials ( ⁇ FR) and means that the heat exchanger stages must be made larger in the new construction of preheaters, even if the system is efficient, even using alternative fuels should be operated.
  • ⁇ FR Alternative Fuels and Raw Materials
  • the invention is also advantageous when a newly designed furnace plant often has to be operated for a long time at very low partial load ( ⁇ 70%), for example in the case of strong fluctuations in the heel.
  • the normally branched partial flow can be turned off and thus the amount of kiln exhaust gas flowing through the heat exchanger stages and thus the gas velocities in the upper heat exchanger stages can be maintained at a normal, reliable level.
  • the speeds in the calciner and in the lowest heat exchanger stage are not affected, which should be taken into account in the interpretation accordingly.
  • the sensible heat of the branched partial stream and possibly the residual stream is utilized.
  • the recovery can be carried out in various ways and according to the particular circumstances, wherein the thermal energy of the furnace exhaust gas can be supplied either the Klinkerher eins- process or external recycling.
  • the diverted partial flow of the furnace gas and the furnace exhaust gas withdrawn from the last cyclone suspension gas heat exchanger viewed in the flow direction of the kiln exhaust gas are mixed with one another.
  • 'It is thus a high-temperature mixed partial flow with a low temperature gas stream, and preferably - used for a raw material and / or fuel drying.
  • the dried fuel or dried raw material is preferably supplied to the clinker production process.
  • the diverted partial flow of the furnace gas and the furnace exhaust gas withdrawn from the last cyclone suspension gas heat exchanger, viewed in the flow direction of the kiln exhaust gas are fed directly to a mixing device. This means that the diverted partial flow is transferred directly into the mixing device and no intervening units are provided for the utilization of the thermal energy.
  • the mixing ratio of the diverted partial flow to the last viewed in the flow direction of the furnace exhaust gas cyclone Schwebegas139 (2004) exhaust gas can be chosen so that the hot gas leaving the mixing device has a temperature of 400 ° C to 550 ° C. If there is no need for material drying, the diverted partial flow of the kiln exhaust gas can be used very efficiently thermally thanks to the high temperature level of preferably> 850 ° C, for example in a waste heat boiler for steam generation.
  • branch line branches off from the flow path according to the first cyclone suspended gas heat exchanger viewed in the direction of flow of the kiln exhaust gas, wherein the branch line branches off from the flow path, in particular between the first and second cyclone suspended gas heat exchangers viewed in the flow direction of the kiln exhaust gas.
  • a Rege ⁇ Lorgan especially a slider for adjusting the partial flow of the diverted furnace exhaust gas.
  • the control element is in this case preferably adjusted so that the volume ratio of diverted partial flow and residual flow of the furnace exhaust gas is 5:95 to 40:60, preferably 10:90 to 30:70.
  • a further preferred development provides that the branch line and a discharge line leading away from the last cyclone suspension gas heat exchanger, as seen in the flow direction of the kiln exhaust gas, are fed to a mixing device.
  • the mixing device is preferably formed by a mixing cyclone whose solids discharge for the precipitated hot meal with the Calciner or a raw meal or transport facility.
  • a further preferred embodiment provides that the kiln exhaust gas branched off via the branch line and, if appropriate, the kiln exhaust gas withdrawn from the last cyclone suspension gas heat exchanger, viewed in the direction of flow of the kiln exhaust gas, are supplied for thermal utilization.
  • the utilization comprises, for example, a raw material and / or fuel drying, wherein the dried fuel or the dried raw material is preferably supplied to the clinker production process.
  • the recovery can also be a steam production in a waste heat boiler um- summarize.
  • a cement clinker production plant in which at a position shown schematically with 1 indicated raw meal in countercurrent to the hot exhaust gases of a clinker furnace 2 preheated in a preheater 3 and calcined in a calciner 4.
  • the clinker leaves the clinker furnace 2 at the point designated 5 and is cooled in a clinker cooler 6.
  • the cooled clinker leaves the clinker cooler 6 at the point designated 7.
  • the preheater 3 may have one or more preheater strands. In the drawing, a strand is shown.
  • the strand has a plurality of " cyclone suspended gas heat exchangers connected in series, the first floating gas heat Exchanger with 8, the last floating gas heat exchanger with 9 and the intervening floating gas heat exchanger are designated 10.
  • the furnace blower 11 generates the required pressure so that the kiln exhaust gas exiting the hot-flour feed side 12 of the rick-rack oven 2 is drawn through the calciner 4 and the pig-gas heat exchangers 8, 10 and 9 connected in series and the hot-gas outlet 13.
  • the Brennstoffaufgäbe for the firing of the calciner 4 is shown schematically at 15.
  • the clinker cooler 6 has a plurality of blowers 25, over which ambient air is blown.
  • the air passes through the clinker cooler 6 and leaves the clinker cooler 6 via the Tertiär Kunststoffabzug 26 and the tertiary air passage 27, wherein the tertiary air duct in the calciner 4 opens.
  • furnace exhaust gas is also removed via a branch line 16.
  • the branch point is located at the outlet 17 of the first floating gas heat exchanger 8.
  • a control element in the form of a slide 18 is arranged, with which the withdrawn amount of furnace exhaust gas can be adjusted.
  • the furnace exhaust gas withdrawn via the branch line 16 is fed to a mixing device 19, for example a mixing cyclone, in which the diverted subset of the kiln exhaust gas is mixed with the residual stream of the kiln exhaust gas withdrawn via the hot gas outlet 13 and drawn through the entire preheater 3.
  • a mixing device 19 for example a mixing cyclone, in which the diverted subset of the kiln exhaust gas is mixed with the residual stream of the kiln exhaust gas withdrawn via the hot gas outlet 13 and drawn through the entire preheater 3.
  • the raw meal is heated to temperatures of 700 to 900, in particular 850 ° C and accordingly, the drawn off via the branch line 16 subset of the furnace exhaust gas has a temperature of about 850 ° C.
  • the residual amount of kiln exhaust gas points after passing the preheater 3 in the hot gas vent. 13 a temperature of 250 to 350 ° C, in particular 300 ° C on.
  • the hot gas leaving the mixing device 19 has a temperature of 400 to 550 ° C., depending on the volume ratio of the exhaust gas flows.
  • the hot gas can now be fed via a line 20 to a dust removal device 21 and the dedusted hot gas to a raw meal drying 22.
  • the hot gas can be supplied via a line 23 to a coal mill 24 for drying the coal provided as fuel for the furnace 14.
  • the partial flow of the kiln exhaust gas branched off via the two-pass 15 and the residual flow withdrawn via the hot gas take-off 13 are not mixed with one another, but are separately supplied to thermal utilization.
  • the withdrawn via the hot gas outlet 13 hot gas is fed via line 20 a raw meal drying 22.
  • the hot gas can be supplied via a line 23 to a coal mill 24 for drying the coal provided as fuel for the furnace 14.
  • the branched off via the branch line 16 hot gas can be supplied due to the much higher temperature of 800 - 900 ° C after a coarse dedusting 31 a waste heat boiler 28 for steam generation.
  • the cooled hot gas leaving the waste heat boiler 28 is then fed via a blower 29 to a further dedusting 30.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Ceramic Engineering (AREA)
  • Materials Engineering (AREA)
  • Structural Engineering (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Furnace Details (AREA)
  • Curing Cements, Concrete, And Artificial Stone (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)

Abstract

L'invention concerne un procédé de fabrication de clinker, selon lequel de la farine crue est préchauffée à l'aide des gaz de fumée chauds d'un four à clinker dans un dispositif de préchauffage (3), et la farine crue préchauffée et éventuellement calcinée dans un calcinateur (4) est brûlée dans le four à clinker (2) pour donner du clinker, le dispositif de préchauffage (3) comprenant au moins une ligne constituée d'une pluralité d'échangeurs de chaleur cycloniques (8, 9, 10) pour l'échange de chaleur entre du gaz et des particules en suspension, traversés les uns après les autres par les gaz de fumée du four, dans lesquels la farine crue est graduellement préchauffée. Selon ledit procédé, une partie du flux des gaz de fumée du four est déviée, de sorte que seul un flux résiduel restant des gaz de fumée est utilisé pour préchauffer la farine crue.
PCT/IB2014/000500 2013-04-15 2014-04-08 Procédé et dispositif de fabrication de clinker WO2014170729A1 (fr)

Priority Applications (11)

Application Number Priority Date Filing Date Title
CN201480034076.4A CN105283428A (zh) 2013-04-15 2014-04-08 用于制造水泥砖的方法和装置
BR112015026061A BR112015026061A2 (pt) 2013-04-15 2014-04-08 processo e dispositivo para a produção de clínquer de cimento
MA38545A MA38545B1 (fr) 2013-04-15 2014-04-08 Procédé et dispositif de fabrication de clinker
MX2015014419A MX364902B (es) 2013-04-15 2014-04-08 Procedimiento y dispositivo de producción de clínker de cemento.
CA2909358A CA2909358A1 (fr) 2013-04-15 2014-04-08 Procede et dispositif de fabrication de clinker
US14/784,331 US10106459B2 (en) 2013-04-15 2014-04-08 Process and device for cement clinker production
KR1020157032680A KR20150143777A (ko) 2013-04-15 2014-04-08 시멘트 클링커 제조 방법 및 장치
EP14723880.2A EP2986579B1 (fr) 2013-04-15 2014-04-08 Procédé et dispositif de fabrication de clinker
RU2015148947A RU2638059C2 (ru) 2013-04-15 2014-04-08 Способ и устройство для производства цементного клинкера
PH12015502364A PH12015502364A1 (en) 2013-04-15 2015-10-12 Process and device for cement clinker production
US16/139,666 US20190039949A1 (en) 2013-04-15 2018-09-24 Process and device for cement clinker production

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ATA307/2013 2013-04-15
ATA307/2013A AT514267A1 (de) 2013-04-15 2013-04-15 Verfahren und Vorrichtung zur Zementklinkerherstellung

Related Child Applications (2)

Application Number Title Priority Date Filing Date
US14/784,331 A-371-Of-International US10106459B2 (en) 2013-04-15 2014-04-08 Process and device for cement clinker production
US16/139,666 Division US20190039949A1 (en) 2013-04-15 2018-09-24 Process and device for cement clinker production

Publications (1)

Publication Number Publication Date
WO2014170729A1 true WO2014170729A1 (fr) 2014-10-23

Family

ID=50721851

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/IB2014/000500 WO2014170729A1 (fr) 2013-04-15 2014-04-08 Procédé et dispositif de fabrication de clinker

Country Status (14)

Country Link
US (2) US10106459B2 (fr)
EP (1) EP2986579B1 (fr)
KR (1) KR20150143777A (fr)
CN (1) CN105283428A (fr)
AR (1) AR096024A1 (fr)
AT (1) AT514267A1 (fr)
BR (1) BR112015026061A2 (fr)
CA (1) CA2909358A1 (fr)
MA (1) MA38545B1 (fr)
MX (1) MX364902B (fr)
PH (1) PH12015502364A1 (fr)
PL (1) PL2986579T3 (fr)
RU (1) RU2638059C2 (fr)
WO (1) WO2014170729A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114656175A (zh) * 2022-03-03 2022-06-24 冀东水泥(烟台)有限责任公司 一种改善水泥适应性的方法

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT512113B1 (de) * 2011-10-25 2016-06-15 Holcim Technology Ltd Verfahren und vorrichtung zum aufarbeiten von nassen, organische komponenten enthaltenden abfallstoffen
DE102014108154A1 (de) * 2014-06-10 2015-12-17 Elex Cemcat Ag Verfahren zur Abgasbehandlung und Anlage mit einer Abgasbehandlungsvorrichtung
CN106403542A (zh) * 2016-11-25 2017-02-15 广东技术师范学院 一种钢铁余热节能型利用装置
CN112654828B (zh) * 2019-08-12 2022-07-22 天津水泥工业设计研究院有限公司 一种水泥预分解窑系统及制备水泥熟料的方法
CN110498622B (zh) * 2019-09-12 2020-10-02 广西四维材料科技股份有限公司 一种粉体多级悬浮预热窑外分解煅烧氧化钙的方法
CN112161485B (zh) * 2020-09-23 2021-05-11 昆明理工大学 一种烧结烟气余热循环利用的方法

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4392822A (en) * 1978-08-02 1983-07-12 Klockner-Humboldt-Deutz Ag System for burning fine-grained material, particularly for the manufacture of cement clinkers

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2833774C2 (de) * 1978-08-02 1984-08-16 Klöckner-Humboldt-Deutz AG, 5000 Köln Brennanlage zur Herstellung von mineralischen Brennprodukten, wie Zementklinker aus Rohmehl
US4298383A (en) 1979-06-25 1981-11-03 National-Standard Company Low viscosity composition for forming shaped bodies
EP0896958B1 (fr) * 1997-08-11 2002-07-17 E. Schwenk Zementwerke KG Procédé pour la production simultanée de clinker de ciment et de courant électrique
JP2002143829A (ja) * 2000-11-10 2002-05-21 Mitsubishi Materials Corp 油混入土の処理方法
DE102004003068A1 (de) * 2004-01-21 2005-08-11 Khd Humboldt Wedag Ag Zementklinkerherstellung mit Teilstromabzug schadstoffhaltigen Drehofenabgases
EP2039663B1 (fr) * 2006-06-28 2013-05-08 Taiheiyo Cement Corporation Appareil de calcination du ciment et procédé d'assèchement de déchets organiques extrêmement aqueux
JP5582554B2 (ja) * 2006-06-28 2014-09-03 太平洋セメント株式会社 セメント焼成装置
JP4478674B2 (ja) * 2006-12-26 2010-06-09 カワサキプラントシステムズ株式会社 セメント焼成プラント廃熱発電システム

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4392822A (en) * 1978-08-02 1983-07-12 Klockner-Humboldt-Deutz Ag System for burning fine-grained material, particularly for the manufacture of cement clinkers

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114656175A (zh) * 2022-03-03 2022-06-24 冀东水泥(烟台)有限责任公司 一种改善水泥适应性的方法

Also Published As

Publication number Publication date
AR096024A1 (es) 2015-12-02
PH12015502364B1 (en) 2016-02-22
CA2909358A1 (fr) 2014-10-23
MA38545A1 (fr) 2016-10-31
MX364902B (es) 2019-05-13
EP2986579A1 (fr) 2016-02-24
RU2015148947A (ru) 2017-05-22
PH12015502364A1 (en) 2016-02-22
MX2015014419A (es) 2016-07-28
PL2986579T3 (pl) 2017-09-29
MA38545B1 (fr) 2017-07-31
US20190039949A1 (en) 2019-02-07
KR20150143777A (ko) 2015-12-23
RU2638059C2 (ru) 2017-12-11
US10106459B2 (en) 2018-10-23
EP2986579B1 (fr) 2017-03-29
CN105283428A (zh) 2016-01-27
AT514267A1 (de) 2014-11-15
US20160052822A1 (en) 2016-02-25
BR112015026061A2 (pt) 2017-07-25

Similar Documents

Publication Publication Date Title
EP2986579B1 (fr) Procédé et dispositif de fabrication de clinker
EP2771302B1 (fr) Procédé et dispositif de traitement de déchets humides contenant des constituants organiques
DE102009041089C5 (de) Verfahren und Anlage zur Herstellung von Zement mit verringerter CO2-Emission
WO2014060275A1 (fr) Procédé d'utilisation de la chaleur perdue d'une installation de production de ciment et installation de production de ciment
DE102016211181A1 (de) Anlage und Verfahren zur thermischen Behandlung von flugfähigem Rohmaterial
EP0707187B1 (fr) Installation pour le traitement thermique de produits en poudre
EP3433558B1 (fr) Installation de production de clinker équipé d'un calcinateur continu à co-courant séparé
DE2820098C2 (fr)
EP0896958B1 (fr) Procédé pour la production simultanée de clinker de ciment et de courant électrique
DE102017012199A1 (de) Gegenstrom-Vorwärmer als Aktivierungssystem vonZementrohmaterialgemisch
EP1996884B1 (fr) Calcinateur à réservoir et son utilisation
DE1758143B2 (de) Mehrstufige anlage zum vorwaermen von zementrohmehl oder aehnlichem feinkoernigem material
AT390249B (de) Verfahren zur verringerung der emission von waehrend der zementherstellung mit dem trockenverfahren insbesondere im waermetauscherbereich gebildetem so2 und vorrichtung zur durchfuehrung des verfahrens
EP1913320A2 (fr) Procede pour prechauffer de la farine crue a ciment et dispositif permettant la mise en oeuvre dudit procede
DE4315212A1 (de) Brennsystem mit Vorcalzinator und Dehydrator
AT200114B (de) Gegenstrom-Rezirkulationsvorrichtung zum Wärmeaustausch zwischen einem Gas und einem feinkörnigen Material
DE19524649A1 (de) Anlage zur thermischen Behandlung von körnigen bis mehlförmigen Rohmaterialien
DE202010011776U1 (de) Brennanlage für Zementklinker mit Vor- und Nachkalzinator
DE2449642A1 (de) Vorrichtung zum brennen von zementrohstoff und aehnlichen massen
DE1027123B (de) Waermeaustauscher zur Waermebehandlung von feinkoernigem Material, insbesondere Kalk oder Zement, durch Gase
EP0318460A2 (fr) Procédé et dispositif pour le préchauffage de matières brutes pulvérulentes
DE2356740B2 (de) Verfahren und Einrichtung zur Herstellung von Zementklinkern od. dgl

Legal Events

Date Code Title Description
WWE Wipo information: entry into national phase

Ref document number: 201480034076.4

Country of ref document: CN

121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 14723880

Country of ref document: EP

Kind code of ref document: A1

DPE1 Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)
REEP Request for entry into the european phase

Ref document number: 2014723880

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2014723880

Country of ref document: EP

ENP Entry into the national phase

Ref document number: 2909358

Country of ref document: CA

WWE Wipo information: entry into national phase

Ref document number: 12015502364

Country of ref document: PH

WWE Wipo information: entry into national phase

Ref document number: MX/A/2015/014419

Country of ref document: MX

WWE Wipo information: entry into national phase

Ref document number: 14784331

Country of ref document: US

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: 38545

Country of ref document: MA

ENP Entry into the national phase

Ref document number: 20157032680

Country of ref document: KR

Kind code of ref document: A

WWE Wipo information: entry into national phase

Ref document number: IDP00201507349

Country of ref document: ID

ENP Entry into the national phase

Ref document number: 2015148947

Country of ref document: RU

Kind code of ref document: A

REG Reference to national code

Ref country code: BR

Ref legal event code: B01A

Ref document number: 112015026061

Country of ref document: BR

ENP Entry into the national phase

Ref document number: 112015026061

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20151014